Absorber demethanizer for fcc process

ABSTRACT

A process for recovering ethylene is disclosed, the process including: recovering a ethylene-containing stream comprising methane, ethylene, and nitrogen oxides from at least one of an ethylene production process and an ethylene recovery process; separating the ethylene-containing stream via extractive distillation using at least one C 2+  hydrocarbon absorbent to produce an overheads fraction comprising methane and nitrogen oxides and a bottoms fraction comprising the at least one C 2+  hydrocarbon absorbent and ethylene; wherein the separating comprises operating the extractive distillation at temperatures and pressures sufficient to prevent any substantial conversion of nitrogen oxides to N 2 O 3 .

CROSS-REFERENCE TO RELATED APPLICATION

This application, pursuant to 35 U.S.C. §120, is a continuation-in-partof and claims benefit to U.S. patent application Ser. No. 12/260,751,filed Oct. 29, 2008. That application is incorporated herein byreference in its entirety.

FIELD OF THE DISCLOSURE

Embodiments disclosed herein relate generally to processes forrecovering ethylene from streams resulting in various petrochemicalprocesses. More specifically, embodiments disclosed herein relate toprocesses for recovering ethylene from ethylene-containing streams asmay be result from ethylene-production or ethylene-recovery processes,where the ethylene-containing stream may contain one or more of carbondioxide, water, and nitrogen oxides. Even more specifically, embodimentsdisclosed herein relate to the recovery of ethylene from streamscontaining methane and nitrogen oxides at conditions to avoidsubstantial formation of N₂O₃.

BACKGROUND

Ethylene is an extremely valuable commodity chemical for producingvarious chemical and polymer products used in numerous commercial aswell as consumer products and applications. Ethylene may be produced ina number of petrochemical processes, including methanol-to-olefins (MTO)processes, fluid catalytic cracking processes (FCC), as well as thermaland steam cracking processes. These processes typically result in aneffluent containing a mixture of hydrocarbons, as well as one or more ofnitrogen, carbon dioxide, nitroxides, methane, ethane, and otherhydrocarbons.

Before the ethylene produced can be sold and used, it is necessary toemploy a process which recovers the ethylene component in a desirable,ethylene-rich stream by separating it from other components andimpurities. Many times this separation is integrated with existingolefins plants but in certain instances, such as where off-gas flowrates are large enough, stand-alone units have also been operated.Because of the high quantity of lighter components such as hydrogen,nitrogen, and methane, the feed gases are typically compressed frompressure of about 1.17 to 1.38 MPa gauge (170 to 200 psig) to pressuresaround 3.45 MPa gauge (500 psig) in multi-stage feed gas compressors.The compression step allows for the recovery of 90% to 99% of theethylene and heavier materials contained in the feed gases using acombination of mechanical refrigeration and expansion of the methane andlighter portions of the feed gas after demethanization. However, thecapital and operating costs for the feed gas compressors are very high.

Further, the processing of refinery off-gases for olefin recovery hasassociated safety concerns because nitrogen oxide is also present intrace amounts in the refinery offgas streams. The nitrogen oxide easilyoxidizes forming nitrogen dioxide. Nitrogen oxides, for example NO andNO₂, are commonly referred to as NOx. Mixtures of nitrogen oxide andnitrogen dioxide can form dinitrogen trioxide (N₂O₃) at temperaturesbelow −21° C. N₂O₃ and heavier diolefins (C₄+) can react at these lowtemperatures forming nitrated gums which are unstable and can explode ifthermally or mechanically shocked.

A typical process for low pressure olefins recovery from fluid catalyticcracker (FCC) offgas is disclosed in U.S. Pat. No. 5,502,971, which ishereby incorporated in its entirety. U.S. Pat. No. 5,502,971 describes alow pressure cryogenic technique for recovering C₂ and heavierhydrocarbons from a refinery off-gas by eliminating feed gas compressionand high pressures while maintaining recovery of C₂ and heavierhydrocarbons at temperatures above temperatures at which nitrated gumscan form.

One process for the separating and recovering of ethylene from a processeffluent involves the use of flash stages and distillation at cryogenictemperatures, as described in U.S. Pat. Nos. 7,166,757 and 4,499,327. Asdescribed therein, the current state of the art ethylene recovery andseparation processes which dominate the industry involve cryogenicboiling point separation of ethylene and methane at temperatures thatmay be lower than −90° C. The cryogenic separation can be very expensivedue to both the capital cost of the specialized vessel metallurgy andrefrigeration equipment, and the operating costs, including compressionand cooling for the energy-intensive chill train.

As discussed, the use of cryogenic temperatures during the processes fortreating refinery off-gas or process effluents can result in unstableand potentially dangerous operating conditions. For example, the NOxpresent in the refinery off-gas can react to form N₂O₃. Further, it hasbeen found that the N₂O₃ formation rate significantly increases withdecreasing temperature, thus making a cryogenic process especiallysusceptible. N₂O₃ is a highly oxidative compound, which can form highlyunstable and highly reactive gums upon contact with poly-unsaturatedcompounds, such as butadiene. Even at cryogenic temperatures and atconcentrations in the ppb levels, such unstable gums can accumulate andcause dangerous runaway reactions and even explosions.

Accordingly, there exists a need for an improved method of separatingmethane to recover ethylene and other valuable products from refineryoffgas that reduces the capital and operating costs and improves theoperation safety and stability.

SUMMARY OF THE DISCLOSURE

In one aspect, embodiments disclosed herein relate to a process forrecovering ethylene, the process including: recovering aethylene-containing stream comprising methane, ethylene, and nitrogenoxides from at least one of an ethylene production process and anethylene recovery process; separating the ethylene-containing stream viaextractive distillation using at least one C₂₊ hydrocarbon absorbent toproduce an overheads fraction comprising methane and nitrogen oxides anda bottoms fraction comprising the at least one C₂₊ hydrocarbon absorbentand ethylene; wherein the separating comprises operating the extractivedistillation at temperatures and pressures sufficient to prevent anysubstantial conversion of nitrogen oxides to N₂O₃.

Other aspects and advantages will be apparent from the followingdescription and the appended claims.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 is a simplified flow diagram of a process for recovering ethyleneaccording to embodiments disclosed herein.

DETAILED DESCRIPTION

Embodiments disclosed herein relate generally to processes forrecovering ethylene from streams resulting in various petrochemicalprocesses. More specifically, embodiments disclosed herein relate toprocesses for recovering ethylene from ethylene-containing streams asmay be result from ethylene-production or ethylene-recovery processes,where the ethylene-containing stream may contain one or more of carbondioxide, water, and nitrogen oxides (NO_(x)). Even more specifically,embodiments disclosed herein relate to the recovery of ethylene fromstreams containing methane and nitrogen oxides at conditions to avoidsubstantial conversion of nitrogen oxides to N₂O₃. As used inembodiments disclosed herein, the term “substantial conversion” inreference to nitrogen oxides refers to the formation and/or accumulationof N₂O₃ at levels greater than 10 ppb in some embodiments, greater than5 ppb in other embodiments, and greater than 1 ppb in yet otherembodiments. Conversely, “prevention of any substantial conversion” orlike terminology refers to the prevention of the formation and/oraccumulation of N₂O₃ at levels greater than 10 ppb in some embodiments,greater than 5 ppb in other embodiments, and greater than 1 ppb in yetother embodiments.

Ethylene-containing streams containing methane, nitrogen oxides, andethylene useful in embodiments disclosed herein may be produced in anynumber of petrochemical processes, and may include effluents oroff-gases from a fluid catalytic cracking system, a thermal crackingsystem; a thermal or steam cracking system, a methanol-to-olefinsprocess, coker processes, visbreaker processes, or combinations thereof.For example, dilute ethylene from a FCC unit may contain very largequantities of hydrogen or methane, if they are not separated at a FCCvapor recovery unit by compression and distillation of FCC off-gas.

The various ethylene production and recovery processes noted above mayproduce streams including one or more C₂ ⁺ streams. In one embodiment,the stream is comprised of C₂ to C₃₀ olefins and/or diolefins. In someembodiments, olefins in these ethylene-containing streams may includeone or more of C₂ to C₈ olefins. In other embodiments, olefins in theseethylene-containing streams may include one or more of C₂ to C₆ olefins.In yet other embodiments, olefins in these ethylene-containing streamsmay include one or more of C₂ to C₄ olefins, for example, ethylene andpropylene. In still other embodiments, olefins in theseethylene-containing streams may consist essentially of ethylene.

In some embodiments, the concentration of ethylene in theethylene-containing streams may be at least approximately 5 molepercent. In other embodiments, the concentration of ethylene in theethylene-containing streams may be at least approximately 10 molepercent. In yet other embodiments, the concentration of ethylene in theethylene-containing streams may be at least approximately 20 molepercent. In still other embodiments, the concentration of ethylene inthe ethylene-containing streams may be at least approximately 30 molepercent.

In some embodiments, the concentration of methane in theethylene-containing streams may be less than approximately 90 molepercent. In other embodiments, the concentration of methane in theethylene-containing streams may be less than approximately 80 molepercent. In yet other embodiments, the concentration of methane in theethylene-containing streams may be less than approximately 70 molepercent. In still other embodiments, the concentration of methane in theethylene-containing streams may be less than approximately 50, 40, 30,20, or 10 mole percent. In other embodiments, the concentration ofmethane in the ethylene-containing stream may be less than approximately2 mole percent.

In order to recover ethylene of sufficient purity, the reactor effluentsand off-gases may undergo one or more separation stages. For example, itmay be desired or necessary to separate ethylene from various reactantsand products, including but not limited to, ethers and alcohols, carbondioxide, water, methane, nitrogen oxides, and other reactants, reactionproducts and by-products, and diluents.

Most hydrocarbon products, byproducts, diluents, and impurities may beseparated from the ethylene in the reactor effluents and off-gases viafractional distillation at non-cryogenic temperatures. For example, ade-propanizer may be used to separate C₃ and heavier materials, and ade-ethanizer may be used to separate ethane and heavier materials fromethylene and lighter materials. In some embodiments, the temperaturesfor such non-cryogenic separations may be higher than approximately −90°C. In other embodiments, the temperatures may be higher thanapproximately −60° C. In yet other embodiments, the temperatures may behigher than approximately −40° C.

A particularly challenging separation is that of ethylene from methaneand other lights (hydrogen, nitrogen, etc.) that may be contained withinthe reactor effluents and off-gases due to their low boiling points.Separating these components using fractional distillation wouldpotentially require cryogenic temperatures less than −90° C. or −100° C.For example, such temperatures may be achieved via a closed-looprefrigeration system using a specialized refrigerant fluid, anadditional refrigeration compressor, and a refrigeration loop.

However, olefin-containing streams produced via such refinery processesmay inevitably contain trace amounts of nitrogen oxides, including NOand NO₂. Typically, nitrogen oxides are inert; however, underappropriate conditions, such as temperatures below about −21° C., thesecompounds may further react to form N₂O₃, which is highly reactive. Forexample, even trace amounts of N₂O₃ may combine and react withpoly-unsaturated olefins, such as butadiene present in anolefin-containing stream, to form highly unstable gum compounds. Attemperatures greater than about −50° C., the rate of N₂O₃ formation maybe negligible. However, it has been found by the present inventors thatthe conversion of nitrogen oxides, including NO and NO₂, to N₂O₃increases with a decrease in temperature, and may become substantial atcryogenic temperatures, for example, at temperatures of less than −90°C. Therefore, traditional methods for separating ethylene fromnitroxide-containing streams using cryogenic flash stages anddistillation may pose safety and operability concerns. Nitroxides andthe potential formation of N₂O₃ are a major safety and operabilityconcern in cryogenic recovery systems, which often operate attemperatures below about −100° C., as they may cause runaway reactionsand even explosions.

It has been found that a hydrocarbon absorbent, such as a C₂₊hydrocarbon absorbent, can be effectively used as an absorbent toseparate and recover the ethylene from the ethylene-containing streamsat non-cryogenic temperatures. For example, ethylene-containing streamsaccording to embodiments disclosed herein can be contacted with ahydrocarbon absorbent in an extractive distillation system, whereby atleast a portion of the ethylene is absorbed by the hydrocarbonabsorbent. The methane and lighter materials may be recovered as anoverheads fraction, and the ethylene and the C₂₊ hydrocarbon absorbentmay be recovered as a bottoms fraction. In some embodiments, thehydrocarbon absorbent may be a C₂₊ hydrocarbon, for example, includingat least one of ethane, propane, propylene, one or more butanes(n-butane, isobutane, etc), one or more butenes, one or more pentenes,and one or more pentanes. In other embodiments, the hydrocarbonabsorbent may consist essentially of propane.

Using a C₂₊ hydrocarbon absorbent to separate ethylene from nitrogenoxides-containing streams at temperatures sufficient to prevent orreduce formation and accumulation of N₂O₃ according to embodimentsdisclosed herein provides a viable alternative to the traditionalcryogenic separation process. In particular, a C₂₊ hydrocarbon absorbentmay be used to separate an ethylene-containing stream produced, forexample, via a FCC process, a coker process, a methanol-to-olefinsprocess, or other processes that may produce an effluent or off-gascontaining NOx, methane and other light gases.

In some embodiments, ethylene recovery systems useful in embodimentsdisclosed herein may include one or more absorber stages. For example,the ethylene-containing stream may be contacted with the hydrocarbonabsorbent in one or more absorber stages arranged in series within asingle column or in a series of multiple columns.

In some embodiments, the ethylene recovery systems may include one ormore extractive distillation and/or distillation stages. For example,the ethylene-containing streams may be contacted with the hydrocarbonabsorbent in one or more extractive distillation and/or distillationstages arranged in series within a single column or in a series ofmultiple columns.

The one or more extractive distillation and/or distillation stages maycomprise trays and/or packing for providing a sufficient surface areafor the contacting. In some embodiments, the ethylene-containing streamsand the hydrocarbon absorbent may be contacted counter-currently in theseparation system. In other embodiments, the ethylene-containing streamsand the hydrocarbon absorbent may be contacted co-currently in theseparation system.

In some embodiments, at least 70 percent of the ethylene in the reactoreffluent or off-gas may be absorbed and recovered from the extractivedistillation system as a bottoms fraction along with the hydrocarbonabsorbent; at least 80 percent of the ethylene may be absorbed andrecovered in other embodiments; and at least 90 percent of the ethylenemay be absorbed and recovered in yet other embodiments.

The bottoms fraction may be further separated to recover anethylene-rich fraction from the hydrocarbon absorbent, such as a C₂₊hydrocarbon absorbent. For example, the ethylene-rich fraction may beseparated from the C₂₊ hydrocarbon absorbent using fractionaldistillation. The concentration of ethylene in the ethylene-richfraction may vary, depending upon the desired end use. In someembodiments, the bottoms fraction may be separated to form an ethylenefraction and a hydrocarbon fraction including at least one of C₂₊hydrocarbon heavier than ethylene. In other embodiments, the bottomsfraction may be separated to form light hydrocarbon fraction containingethylene and ethane, and a hydrocarbon fraction containing at least oneC₃₊ hydrocarbon.

As used herein, “rich” fractions contain at least 50% by weight of theindicated component. In some embodiments, the ethylene-rich fraction maycontain at least 90% ethylene; at least 95% ethylene in otherembodiments; at least 98% ethylene in other embodiments; at least 99%ethylene in other embodiments; at least 99.5% ethylene in otherembodiments; and at least 99.8% ethylene in yet other embodiments. Thetargeted concentration of the indicated component in the streams maydepend upon downstream requirements; for example, where the ethylene isto be used in a polymerization process, “polymer grade” ethylene,containing greater than 99% by weight ethylene, may be required.

In some embodiments, the concentration of the carried over hydrocarbonabsorbent recovered in the overheads fraction along with methane fromthe extractive distillation system is less than approximately 30 molepercent. In other embodiments, the concentration of the carried overhydrocarbon absorbent recovered in the overheads fraction along withmethane from the extractive distillation system is less thanapproximately 15 mole percent. In yet other embodiments, theconcentration of the carried over hydrocarbon absorbent recovered in theoverheads fraction along with methane from the extractive distillationsystem is less than approximately 10 mole percent. In still otherembodiments, the concentration of the carried over hydrocarbon absorbentrecovered in the overheads fraction along with methane from theextractive distillation system is less than approximately 5 molepercent.

Embodiments disclosed herein maintain pressure and temperature insidethe absorber or extractive distillation system sufficient to prevent anysignificant formation of N₂O₃ from nitrogen oxides, including NO andNO₂, present in the ethylene-containing streams. As discussed above, ithas been found that the rate of N₂O₃ formation becomes significant attemperatures below approximately −90° C. Thus, by avoiding cryogenicprocess temperatures of approximately −90° C. and below, for example, byusing a hydrocarbon absorption process according to embodimentsdisclosed herein, the formation of N₂O₃ may be prevented orsignificantly reduced.

In some embodiments, the absorber or extractive distillation system maybe operated at an overheads temperature of −90° C. or greater; at anoverheads temperature of −50° C. or greater in other embodiments; −40°C. or greater in other embodiments; −20° C. or greater in otherembodiments; −10° C. or greater in other embodiments; and at anoverheads temperature of 0° C. or greater in yet other embodiments.

In general, the overheads pressure inside the absorber or extractivedistillation system may be maintained at a level required for thedistillation and as required for absorption of ethylene into thehydrocarbon absorbent. In some embodiments, the overheads pressureinside the absorber or extractive distillation system may be in therange from 0.01 MPag to 10 MPag; in the range from 0.1 MPag to 4 MPag inother embodiments; from 0.5 MPag to 3 MPag in other embodiments; and theoverheads pressure inside the absorber or extractive distillation systemmay be in the range from approximately 0.5 MPag to 1 MPag in yet otherembodiments.

Referring now to FIG. 1, an extractive distillation process inaccordance with embodiments disclosed herein is illustrated. Forsimplicity purposes, auxiliary equipment has been omitted from thefigure. One of ordinary skill in the art would recognize that otherequipment and devices, including but not limited to, pumps, compressors,heat exchangers, drums, vessels, reactors, flow lines, valves, andcontrol loops, can also be used. For example, other features notillustrated in FIG. 1, including but not limited to, internal orexternal heat exchange loops on the extractive distillation column andother features that may be used and could appear in a Process &Instrumentation Diagram (P&ID) for embodiments disclosed herein,although not illustrated, may be used in accordance with embodimentsdisclosed herein.

An ethylene-containing stream may be supplied to an extractivedistillation system 10 via flow line 102. The extractive distillationsystem 10 may be an absorption column in some embodiments of theinvention and the ethylene-containing stream 102 may enter theextractive distillation system 10 at a suitable point in the system toeffect the desired contact with the C₂₊ hydrocarbon solvent fed via flowline 104. For example, the solvent stream 104 may be fed to theextractive distillation system 10 at a point above the inlet for stream102, such that the hydrocarbon solvent flow is countercurrent to themethane, i.e., the solvent flows down the extractive distillation systemto contact the ethylene-containing stream 102 countercurrently. As thehydrocarbon absorbent traverses down the column, ethylene is absorbed bythe hydrocarbon absorbent. The hydrocarbon absorbent and the absorbedethylene may be recovered from the column 10 as a bottoms fraction viaflow line 108. The methane may be recovered from the column 10 as anoverheads fraction via flow line 106. In some embodiments, at least aportion of the overheads fraction 106 may be returned to the column 10as reflux via flow line 112.

The bottoms fraction 108 may be further treated (not shown in FIG. 1) toseparate an ethylene-rich fraction containing ethylene and a hydrocarbonfraction containing the hydrocarbon absorbent. At least a portion of thehydrocarbon fraction may be recycled to the column 10 as the hydrocarbonabsorbent 104 or a hydrocarbon absorbent make-up stream 114.

In some embodiments where the hydrocarbon absorbent is propane and theoverheads fraction 106 from the column 10 comprises propane, at least aportion of the overheads fraction 106 may be used as fuel. For example,both the methane and the propane in the overheads fraction 106 may besent to a fuel header. In other embodiments, at least a portion of thepropane in the overheads fraction 106 may be compressed and recovered.In yet other embodiments, the overhead fraction 106 may be furthertreated in a vent condenser (not illustrated) to increase olefin(ethylene) recovery.

In addition to methane and nitroxides, as mentioned above, theethylene-containing streams may contain one or more additionalcomponents, such as diluents and reaction byproducts, including helium,argon, nitrogen, carbon monoxide, carbon dioxide, water, paraffins suchas methane, ethane, and propane, aromatic compounds, and mixturesthereof. Additionally, air may be entrained into an ethylene productionor recovery process, for example, due to operation under partial vacuumconditions or as an impurity in one of the feedstock components.Ethylene-containing streams may also include non-olefin products,including but not limited to, paraffins, acetylenes, ethers, alcohols,and esters.

In some embodiments, at least a portion of the ethylene-containingstreams may be fed to an extraction system for removing any oxygenates,such as methanol and/or ethers contained therein, using an aqueoussolvent, such as water or glycol. An aqueous fraction having anincreased concentration of methanol and ethers may be recovered from theextraction system. A hydrocarbon phase comprising methane and ethylene,and lean in methanol and ethers, may be recovered from the reactoreffluent in the extraction system. The hydrocarbon phase may then besent for further component separation(s). In some embodiments, theethylene-containing streams may be compressed prior to anyseparation(s).

Carbon dioxide that may be present in the ethylene-containing streamsmay also require removal. For example, an olefin product specificationmay require removal of carbon dioxide from the ethylene-containingstreams. Further, exposure of the carbon dioxide containing stream tobelow-sublimation temperatures may result in equipment damage and frozenpiping. Methods commonly known and used in the industry, such as causticsolution treatment or amine absorption, may be used to remove CO₂ fromthe ethylene-containing streams. In some embodiments,ethylene-containing streams may be contacted with a caustic solution toseparate at least a portion of the carbon dioxide present in theethylene-containing streams. If necessary, the ethylene-containingstreams may be compressed prior to the carbon dioxide removal stage.

The presence of water in ethylene-containing streams may lead to anumber of problems. For example, cooling and/or compressing theethylene-containing streams may result in formation of water condensatethat can damage equipment and freeze pipes. Therefore, dehydration ofthe ethylene-containing streams to remove water using one of a number oftechniques commonly used in the industry may be required or may beoptionally performed based on process schemes and temperatures employed.In some embodiments, a molecular sieve dryer may be used for separatingat least a portion of the water, drying the ethylene-containing streams.In other embodiments, a chemical desiccant such as glycol may be usedfor drying the ethylene-containing streams. In yet other embodiments, aportion of the water in the ethylene-containing streams may be condensedand the remaining ethylene-containing streams may be dried. Otherdehydration techniques commonly known and used in the industry may alsobe used. If necessary, the ethylene-containing streams may be compressedprior to the water removal stage.

Advantages of processes according to embodiments disclosed herein mayinclude improved operational safety and stability due to minimization ofN₂O₃ formation from nitrogen oxides. As discussed above, trace amountsof nitrogen oxides, including NO and NO₂, present in theethylene-containing streams can react to form N₂O₃, a highly oxidativecompound which can in turn react with heavy unsaturated compounds, suchas butadiene, present in the ethylene-containing streams to formunstable and highly reactive gums. Such gums, even at cryogenictemperatures and at ppb concentrations, can accumulate and causedangerous runaway reactions and even explosions. As the rate of N₂O₃formation drastically increases with decreasing temperature, and thusthe cryogenic processes at temperatures lower than approximately −90° C.currently used for separation of methane from ethylene-containingstreams are a major safety concern. In contrast, Applicants have foundthat using hydrocarbon absorption to separate methane fromethylene-containing streams at temperatures of −90° C. or higher issufficient to prevent formation of N₂O₃.

Another advantage of processes according to embodiments disclosed hereinmay include reduced capital equipment cost. For example, the traditionalcryogenic process, commonly referred to as the “chill train,” requiresspecialized metallurgies and complicated refrigeration systems,including vessels, compressors, heat exchangers, circulation piping, andrefrigerant costs. In contrast, as the present process is not conductedat cryogenic temperatures, less expensive metallurgy can be used and anumber of equipment items associated with the chill train may beeliminated.

Processes according to embodiments disclosed herein may alsoadvantageously reduce operating costs. For example, the energy costs ofthe refrigeration compression associated with the traditional cryogenicseparation system may be considerably higher than those associated witha non-cryogenic extractive distillation process.

Still another possible advantage of recovering ethylene and/or heavierolefins from ethylene-containing streams according to embodimentsdisclosed herein may be that any portion of the C₂₊ hydrocarbonabsorbent, such as propane, entrained with the distillate, does notrequire additional compression and recovery, and instead may be sentdirectly to the process plant fuel header or otherwise may be used as afuel. For example, in other demethanizer processes, the value of anyresidual C₂₊ 0 hydrocarbons may be too high to be sent to fuel;requiring additional compression and recovery facilities to recover thevalued products. In contrast, the C₂₊ hydrocarbons have no further usein the present processes, and thus may economically be sent to fuel.

Recovery of ethylene and/or heavier olefins from ethylene-containingstreams according to embodiments may also reduced capital and operatingcosts due to reduced separation requirements for other non-olefincomponents present in an ethylene-containing streams. For example,limiting the process design to operating temperatures of −90° C. andhigher, and in some embodiments to temperatures of −40° C. and higher,may eliminate the need for expensive methane refrigeration loopscommonly used in cryogenic separation schemes. In contrast, usingpropane and/or propylene refrigeration to provide chilling for processesaccording to embodiments disclosed herein may substantially reducecapital investment costs, reduce operating costs, and improvereliability.

While the disclosure includes a limited number of embodiments, thoseskilled in the art, having benefit of this disclosure, will appreciatethat other embodiments may be devised which do not depart from the scopeof the present disclosure. Accordingly, the scope should be limited onlyby the attached claims.

1-14. (canceled)
 15. A process for recovering ethylene, the processcomprising: recovering a ethylene-containing stream comprising methane,ethylene, and nitrogen oxides from at least one of an ethyleneproduction process and an ethylene recovery process; separating theethylene-containing stream via extractive distillation using a solventcomprising a C₂-C₅ hydrocarbon absorbent to produce an overheadsfraction comprising methane and nitrogen oxides and a bottoms fractioncomprising the solvent and ethylene; wherein the separating comprisesoperating the extractive distillation at temperatures and pressuressufficient to prevent any substantial conversion of nitrogen oxides toN₂O₃.
 16. The process of claim 15, wherein the ethylene-containingstream comprises at least one of an effluent from a fluid catalyticcracking system, an effluent from a thermal cracking system; an effluentfrom a steam cracking system, an off-gas from a fluid catalytic crackingsystem, an off-gas from a thermal cracking system, an off-gas from asteam cracking system, an off-gas from a methanol to olefins conversionsystem, or combinations thereof.
 17. The process of claim 15, whereinthe C₂-C₅ hydrocarbon absorbent comprises at least one of ethane,propane, propylene, one or more butanes, one or more butenes, one ormore pentanes, one or more pentenes, and mixtures thereof.
 18. Theprocess of claim 15, further comprising operating the extractivedistillation at an overheads temperature of −90° C. or greater.
 19. Theprocess of claim 15, further comprising operating the extractivedistillation at an overheads temperature of −40° C. or greater.
 20. Theprocess of claim 15, further comprising operating the extractivedistillation at an overheads pressure in the range from about 1 to about4 MPag.
 21. The process of claim 15, further comprising separating thebottoms fraction to form an ethylene fraction and a hydrocarbon fractioncomprising the C₂-C₅ hydrocarbon absorbent.
 22. The process of claim 21,further comprising recycling at least a portion of the hydrocarbonfraction to the extractive distillation.
 23. The process of claim 15,further comprising separating the bottoms fraction to form a lighthydrocarbon fraction comprising ethylene and ethane, and a hydrocarbonfraction comprising at least one C₃₊ hydrocarbon.
 24. The process ofclaim 16, further comprising at least one of: contacting theethylene-containing stream with a caustic solution to separate at leasta portion of any carbon dioxide contained in the ethylene-containingstream prior to the separating; contacting the ethylene-containingstream with a molecular sieve dryer to separate at least a portion ofany water contained in the ethylene-containing stream prior to theseparating; recovering an ethylene-containing stream having a reducedconcentration of at least one of carbon dioxide and water; and feedingthe ethylene-containing stream having a reduced concentration of atleast one of carbon dioxide and water as the ethylene-containing streamfed to the separating.
 25. The process of claim 15, further comprising:condensing and recycling at least a portion of the overheads fraction tothe extractive distillation as a reflux.
 26. The process of claim 15,further comprising treating the overheads fraction in a vent condenserto increase ethylene recovery.